High efficiency heat pump combining absorption and solution concentration change

ABSTRACT

High efficiency heat pump combining absorption and solution concentration change. The method gives a few times higher efficiency for heat transfer applications like heating—air conditioning. It is a heat and mechanical compression method using liquid electrolyte solutions, combining steam absorption, solution concentration change and mechanical compression. There is no heat consumption. Steam condensation is performed by a high concentration solution and vaporization from a low concentration solution reducing in this way the required mechanical compression of the known refrigeration cycle. The method may be used for work production too, exploiting moderate temperature heat sources.

The common way of heat transfer to higher temperature, as in cooling—refrigeration applications, is by using the steam expansion—compression cycle. The refrigerant vaporizes at pressure p₂ absorbing heat from its environment (a low temperature heat source), is compressed to a higher pressure p₁, condensed rejecting heat at higher temperature T1 (high temperature heat source) and expands at the initial pressure p₂.

The refrigerant is a pure substance. The vaporization and condensation temperature of a pure substance are the same. The higher the pressure the higher the vaporization temperature. Steam compression reflects the electric energy consumption of the cycle.

There is also an application where heat compression is applied. Now heat is consumed for working fluid compression. The solution is partially vaporized at high temperature.

The steam performs a cooling cycle while the solution expands and returns to absorber where the steam is absorbed (condensed) at low temperature. The initial solution has been reformed, compressed and driven to evaporator. The application is called absorption or heat compression heat pump. The working fluid is a solution instead of a pure substance. The most common solutions are NH₃—H₂O and LiBr—H₂O. The vapor pressure of a solution is a function of temperature and concentration as well. Ideal solutions follow the Raoult low P=xP₀, where P₀ the vaporization pressure of the pure substance at a given temperature and x the concentration. Real solutions divers from this low and P=αP₀=γmP₀, with a the activity, γ the activity coefficient being a function of concentration and m the mole concentration. It means that at a given temperature the solution may vaporize at different pressure depending on the concentration. The steam is absorbed by the solution and thus condenses. In the followings the term steam absorption or condensation is used. The compression ratio is DP=p₁/p₂ =α₁p₀₁/α₂p₀₂=(α₁/α₂)(p₀₁/p₀₂). The ratio α₁/α₂ is unit in the usual absorption cycle as the solution has the same concentration during vaporization and condensation.

In the present method this ratio is less than ⅕. In an extreme case this ratio may equals 1/(p₀₁/p₀₂) and DP=1. It means that for the same temperature lift the compression ratio and consequently the required work will be less by a proportional ratio. Activity decreases as the electrolyte concentration increases. In our cooling application we prefer solutions with negative deviation from Raoults low, it is the vapor pressure is lower than that of the ideal solution. Exothermic heat of reaction is also preferred. There are many solvent—solute combinations that may be used. In the following description we refer to the solute as electrolyte and especially as a solid electrolyte. Electrolyte solutions seem to be the most convenient while other kind of solutes can also be used. There are two pressure levels in absorption cycle as in the mechanical (electrical) compression cycle. The advantage of the first is that liquid compression spends much lesser electric energy than vapor compression and heat is cheaper than electricity. In our method there is no considerable heat consumption too.

Heat is absorbed by the evaporator to produce steam and rejected by the absorber where steam is absorbed (condensed). The temperature rise depends on pressure ratio ΔP.

Cooling efficiency COP of the absorption cycle is the evaporation heat of the pure solvent divided by that of the solution. The last is higher than the first and usually COP=0.7.

In the present method of working fluid compression for heat transfer, the evaporating and condensing solutions differ as much as possible in (electrolyte) concentration, with condensation taking place in the most concentrated (higher concentration) solution so that a lower ΔP is achieved for the same temperature levels. The partial solution evaporation takes place at lower temperature than the condensation in reveres to classical absorption cycle. We name the high solute concentration solution as rich solution and the low electrolyte concentration, poor solution. The solution concentration change is achieved by solution temperature change. The solubility of many electrolytes is reduced by decreasing temperature. As an example, RbNO₃ (M=1,3−30) for t=0 to 100° C., KBr (M=4−12) for t=0 to 160° C., TINO₃ (M=1−15) for t=0 to 100° C. We select such an electrolyte for the description that follows. The term concentrated solution refers to the maximum concentration at a given temperature. The solute may be any substance dissolved in the solvent. The most convenient solutes for the application are the electrolytes. For this reason the term electrolyte is used to the followings instead of solute. A high concentration, concentrated (saturated) solution (rich) is cooled from a high temperature to a lower (environment) temperature. During this process an amount of the dissolved substance (electrolyte) forms a different phase like sediment (crystals) and is separated from the solution by any of the known methods. The remaining liquid solution has lower electrolyte concentration (poor solution). (If a solution which solubility decreases increasing temperature is used, the solution is heated from the low temperature to separate the electrolyte. The poor solution is at highest temperature). Its pressure is regulated (expanded) so as to vaporize at the desired temperature for a given concentration. In this way the poor solution is partially evaporated in evaporator (E) absorbing heat from its environment (low temperature heat sink) and causing refrigeration. Steam is compressed and driven to a heat exchanger, the absorber (A) where the separated electrolyte and the remaining poor solution of the evaporator also enter after having been compressed. The initial rich (higher concentration) solution has been reformed. Condensation takes place by rejecting heat from the absorber at high temperature. The steam may be absorbed by part of the separated phase at high temperature and the result enters a condenser with the poor solution from the evaporator and the rest of separated phase to reform the initial solution which will be cooled again. All of the streams have come to the same pressure before joining each other. In case of using an electrolyte having endothermic solution, part of the separated electrolyte is being driven to the remaining poor solution moving from the evaporator to absorber.

Separation and dissolution of different phase into the temperature changing solution may take place at the same equipment. Crystals remain on the equipment in one stream (cooled stream) and dissolved as the other stream (heated stream) passes from the same surface. The required dissolution heat is recovered through a heat exchanger from the solution that is cooled going the opposite way. Heat exchange takes place between heating and cooling solutions to recover heat.

More than one cycles can be combined for higher temperature lift. The evaporator of the second cycle, which works at higher temperatures than the first, recovers heat from the absorber of the first.

In any case the being cooled solution, may be cooled at below environment temperature. The partial evaporation there takes heat from the solution and cools it at the lower temperature. In this way its temperature and consequently the concentration is further reduced. The resulting electrolyte joins the rest separated amount and the steam is driven to the being cooled solution or to separated electrolyte. The remaining solution is compressed and evaporated at the desired temperature as before.

The method is presented in FIG. 1 where the dissolution of the separated electrolyte takes place in two parts, into the equipment-absorber (A1) and the poor solution returning to (A1). The rich solution from (A1) is cooled from temperature TA to the environment temperature Tamb through the heat exchanger (HE) (point 1 to 2). The concentration changes from M_(A) to M_(E) and the separated electrolyte is selected to a box (K1). The remaining poor solution is expanded and partially vaporized at the evaporator (E) absorbing heat from its environment. An additional amount is separated (since a concentrated solution is evaporated) and selected to (K2) and from there to (K1). The produced steam is compressed and coming to the absorber (A1) (point 4) to be absorbed (condensed) by the electrolyte coming from (K1) (point 6). Heat is rejected at temperature TA. The remaining solution of the evaporator (point 3) is compressed and heated through (HE) and driven to equipment (A1) while the rest of the separated electrolyte has been dissolved into it. All of the separated phase may be dissolved into (A1) instead of the poor solution. Heat is also rejected. The initial solution has already been reformed. The poor solution going from (E) to (A1) consumes heat to increase its temperature from TE to TA. This heat is mc_(p)Δt where m the mass, cp the specific heat and Δt the temperature change (TA−TE). A similar amount of heat is rejected by the rich solution cooled from TA to TE. Steam increases its temperature also through heat exchanger (HE). Electrolyte is crystallized as rich solution is cooled and crystallization heat is absorbed. This may happen at low temperature. Part of this heat is rejected (as dissolution heat) from (A1) during steam condensation. Solution heat is balanced by crystallization heat that is theoretically the same. Refrigeration is caused by steam evaporation at the evaporator (E) and heating by dissolution and condensation in (A1). Condensation heat equals evaporation heat increased by the stated heat of solution. The energy balance gives:

Input energy Qin=heat of solvent vaporization q_(L)+electrolyte crystallization heat q_(k)+electric energy for steam compression w_(el).

Output energy Qout=solvent (steam) condensation heat q_(L)+electrolyte dissolution heat q_(k1) in (A1) by steam+dissolution in poor solution q_(k2), Qout=−(q_(L)+q_(k)).

The result is heat transfer from low temperature TE (environment temperature or lower in refrigeration applications) to a higher temperature TA almost without heat consumption. Depending on the solution used and the specific application a small amount of electric energy is consumed. This amount is a few times less than that required by a conventional compression cycle. If steam is absorbed only by separated phase in a secondary absorber and the result joins the poor solution in (A1), the condensation temperature may be very high as the solution formed in secondary absorber has a very high concentration.

In any cycle form, if an electrolyte with endothermic heat of solution is used, part of the separated electrolyte from (K1) is dissolved in the solution moving from (E) to (A) recovering heat from the solution moving the opposite way.

In order to achieve higher temperature lift two similar cycles may be combined. The evaporator of the second cycle recovers heat from the absorber of the first. Suppose the first cycle works between 0° C. and 120° C. and the second between 120° C. and 250° C.

A lift from 0° C. to 250° C. has been achieved. The rich solution of the second cycle may be cooled below its evaporator temperature as this temperature is higher than the environment temperature. As an example one of the referred electrolytes may be used for the first cycle and PbNO₃ for the second (M=3.8 at 100° C. and 8 at 200° C.).

An alternative of the above cycle is presented in FIG. 2. The poor solution from point 2 is heated at the temperature of the available heat source, expanded and evaporates. The solution after partial evaporation is cooled again to separate additional solute and returns to evaporator. The solution is driven to absorber from another exit as before.

The additional solute joins (K1). Alternatively the evaporator (E) can be used as an auxiliary evaporator. The produced steam is condensed and enters the main evaporator at the lower refrigeration temperature together with the remaining from (E) solution.

Here the solution is vaporized to cause the refrigeration. Steam and remaining solution move to the absorber as before. The main evaporator has a solution that is not concentrated. The poor solution can split into two flows. The first enters directly to main evaporator and the second is driven to the auxiliary evaporator.

Another alternative is presented in FIG. 3 where the temperature TA of the absorption-dissolution equals TE (evaporation). In practical applications TA is a little higher than TE so as condensation heat may be transferred from the absorber to evaporator. The produced steam (point 6) is expanded through the turbine (TU1) producing work and then rejects heat through condenser (CON) and is condensed. Expands and evaporates in pure solvent evaporator (EV). In this application beyond the solution vaporization and condensation, pure solvent evaporation and condensation takes place. Next, the steam is superheated, compressed by compressor (TU2) at the pressure of (A1) (if (A1) pressure is higher than that of (EV) and enters absorber (A1) (point 7), where separated electrolyte from (K) enters too (point 5). The remaining solution of the evaporator is driven to (A2) where the rest of the separated electrolyte enters too. The solution formed at (A1) is compressed and enters (A2). The initial rich solution has been reformed. This is the solution that is cooled for the electrolyte to be separated as stated above. For simplicity, equipments (A1) and (A2) may build in one equipment, the absorber (A1). The separated electrolyte dissolves into the remaining from the evaporation solution, compressed and enters the absorber (A1) with steam, forming the initial solution. The poor solution, after electrolyte separation and before entrance to evaporator, recovers heat from the rich solution leaving absorber, through heat exchanger (HE). To make it possible, further cooling of the last solution takes place through an additional heat exchanger, or by partial evaporation of this solution to a lower temperature. In case an electrolyte exhibiting endothermic heat of solution is used, the remaining after evaporation solution may be cooled at the lower temperature and heated again. Separated phase is dissolved into the poor solution as it returns to absorber after cooling. This solution has now high concentration.

Turbines (TU1) and (TU2) are used to control the condensation (heating) and evaporation (refrigeration) temperature of (CON) and (EV). These turbines may be connected so that the work of the first is used by the second. In this cycle compression is achived through (E), (A) and (K). The compression ratio is α1/α2=α_(E)/α_(A).

Additional mechanical steam compression may be applied also.

FIG. 4 is a drawing showing the relation between temperature T and pressure P for a given solution concentration (ME is the concentration of low concentration solution of the evaporator and M_(A) the high concentration of the absorber solution). Both equipments work at temperature TE=TA, while the pressure of the evaporator is P_(E) and of the absorber P_(A).

Energy balance gives that the consumed energy is recovered by rejected energy.

Solution evaporation heat is recovered by solution condensation heat, solvent evaporation is performed by exploiting environmental heat and crystallization by dissolution heat. Steam compression is achieved by a crystallization—dissolution cycle which spends no heat (theoretically).

A double or multi stage cycle may be applied here too. In each cycle, a pressure difference between evaporator—absorber is created by the above method. Each cycle works in different pressure levels. Different or the same solutes and the same solvent are used in each cycle. The evaporator pressure of the second cycle is close (preferably equal) to the absorber pressure of the first and the absorber pressure of the second close (preferably equal) to evaporator pressure of the first. The steam of the second cycle evaporator performs the refrigeration cycle described above (condensed—expands—evaporates) and enters the absorber of the first cycle. The steam of the first cycle evaporator enters the absorber of the second. Now higher thermal compression has been achieved. Condensation heat is also recovered by evaporation heat. The cycles do not necessarily work at the same temperatures. Additional mechanical compression may be applied to steam in order to enter the absorber. Suppose the absorber of the first cycle works at 0.1 bar, the evaporator at 1 bar and the absorber of the second at 1 bar and its evaporator at 10 bar. The steam of the second evaporator is at 10 bar and expands to 0.1 bar. The steam of the first evaporator is at 1 bar and enters the second absorber at the same pressure of 1 bar. The after all compression ratio is 10/0.1=100.

Equipments (A) and (E) may be the same equipment. The flow to be evaporated and the flow to be condensed may pass through the same heat exchanger. The application may be applied for work production. The steam from the evaporator is expanded through a steam turbine to produce work instead of performing the refrigeration cycle.

As the expansion ratio is low for power production, steam may be absorbed by the separated electrolyte at low temperature. The resulting substance is driving to an equipment (A), where the remaining poor solution from the evaporator enters too to form the initial rich solution. In this case heat is consumed to evaporate the solution since the absorption heat is rejected at lower temperature. Electrolytes which crystals are connected with solvent molecules at low temperature but not at higher temprature, are preferred here. The advantage is that the expansion ratio is higher than that of the known power cycle at the same temperature.

Many solvents like H2O, methanol, formamide, formic acid, acetonitrile, DMF, DMSO can be combined with many electrolytes like ZnCl2, SbCl2, SbF2, CoI2, TICl, (Li,Na,K,NH4 etc) with (Cl,Br,I,SO4 . . . ),Pb(NO3)2, TI(NO3), RbNO3.

Solutes which concentration decreases increasing temperature may be used. KBr—NH3 is an example. The high concentration solution is at low temperature and the concentration decreases as the solution is heated. Solute is separated again. The high temperature solution is vaporized. The steam performs the known condensation—expansion—vaporization cycle and enters absorber. The remaining solution returns to absorber recovering heat from the solution moving the opposite direction. The separated solute enters absorber too, forming the initial solution. Now vaporization heat is required. Alternatively the steam may be absorbed by the separated solute and then enter absorber. The solute may be NH3, Freon or other non electrolytes. The same may be used for work production. The steam is expanded through a turbine instead of performing the cooling cycle. 

1. Method for working fluid compression for heat transfer from a lower to a higher temperature heat sink using a heat compression absorption pump where the working fluid is a solution of substances in a liquid solvent which is partially vaporized and then condensed and the absorption solution concentration changes by absorption solution temperature lowering so as part of the absorbent is separated, characterized by the fact that the absorbent separation from the absorber leaving solution, takes place without energy consumption, the heat rejection from the concentration lowering solution is fully recovered, the absorber solution is concentrated and at high absorbent concentration. The method works effectively at high, at a range of 1/10 or higher, absorber/generator concentration ratio and activities ratio. Temperature lift may be high, in the range of 150-200° C. The method works between two pressure levels offering a high compression ratio. After absorbent separation, the solution is expanded, offering heat absorption from any lower than the ambient temperature and then steam and remaining liquid solution is compressed at high pressure. A liquid solution concentrated in dissolved substances like electrolytes, is being cooled to a lower temperature (FIG. 1, point 1 to 2) so that its concentration changes and a different phase, like crystals, are formed, separated from the solution and stored in a container (K1). The resulting low concentration solution is expanded so as it is partially vaporized at the desired refrigeration temperature (E). The produced steam is heated through a heat exchanger (HE), compressed to the absorber pressure and enters absorber (A1). An additional amount of different phase may be separated during vaporization (K2) and driven to container (K1). The remaining solution is compressed and heated through the heat exchanger (HE) recovering heat from the solution leaving the absorber and enters absorber (A1). The same happens to the separated phase. Now the initial, high concentration solution has been reformed. Heat is rejected from the absorber. The initial solution may be created at two separated equipments, both at high temperature. The steam is absorbed by a portion of the separated substance and the rest of this substance is dissolved in the poor solution. The solution from the absorber is compressed and mixes with the returning from the evaporator solution to create the initial solution. Alternatively, part of the separated phase may enter the low concentration solution moving from the evaporator to absorber so that its concentration increases gradually. The solution that leaves absorber maybe cooled at a much lower than environment temperature by expansion to a convenient pressure. The steam is driven to the container (K1) or to the solution, the additional separated phase enters (K1) while the solution recovers heat from the cooling solution, compressed and expanded to the desired refrigeration temperature (E). A higher concentration difference between evaporator and absorber solutions is achieved in this way. Water is the most common solvent. Many other solvents can be used too. Methanol, monomethylamine, dimethilsulfoxide, DMF, acetonitrile, formamide, formic acid, are convenient too. Many electrolytes like CoI2, Pb(NO3)2, TICl, RbNO3, TINO3, ZnCl2, SbCl2, SbF2, (Cl, Br, I, SO4) with(K, Na, NH4, Li, . . . ) can also combined with any solvent.
 2. The method for heat transfer as in claim 1 characterized by the fact that the low concentration solution (FIG. 2, from point 2) is heated and then vaporized at a higher temperature in the evaporator (E). The remaining solution is cooled again to the lower temperature to separate additional different phase, reheated and returns to evaporator. Heat exchange between the two solutions takes place here too. It helps to upgrade a higher than environment temperature heat sink and avoid crystallization during evaporation. Alternatively, the evaporator (E) can be used as an auxiliary evaporator. The produced steam is condensed and enters the main evaporator at the lower refrigeration temperature with the remaining from (E) solution. Here the solution is vaporized to cause refrigeration. Steam and remaining solution move to absorber as before. The main evaporator has a solution that is not concentrated. In this case the low concentration solution (point 2) may be separated into two streams, the first entering the auxiliary evaporator and the second moving to the main evaporator. At the end of solution cooling (point 2), external cooling of a few degrees is applied.
 3. The method of heat transfer as in claim 1 characterized by a combination of many similar cycles. The heat of the absorber of the first cycle, which cycle works at lower temperatures, is used by the evaporator of the second cycle which works at higher temperatures. The solution of the second cycle that leaves its absorber is cooled at a temperature lower than that of its evaporator. This combination results in a higher temperature lift. In the case the two cycles use the same solvent, the steam of the first evaporator is compressed and enters the absorber of the second cycle while the steam of evaporator of the second cycle enters the absorber of the first. The temperature of the absorber of the first cycle is close to the temperature of the evaporator of the second so as heat transfer is possible.
 4. A method for thermal compression of a working fluid for heat transfer to higher temperature by solution concentration change as in claim 1, characterized by the fact that the partial vaporization takes place at a little lower than the absorption temperature so that condensation heat is recovered by vaporization. After cooling, the low concentration solution is heated again recovering heat (FIG. 3, HE) from the cooling stream and vaporizes (E). Part of the separated phase as well as the vapor after performing the cooling cycle stated below, are compressed and enter the absorber (A1). The remaining solution from the evaporator enters a collector (A2) with the rest of the separated phase which is dissolved there. The solution from the absorber is compressed and enters the collector too. The initial solution has been reformed in the collector and the cooling process starts again. Instead, all of the separated phase enters the collector (A2) and then the solution is compressed to absorber pressure and enters there to absorb steam and form the initial solution. Alternatively the solution leaving evaporator may be cooled and heated again. Separated phase is dissolved in this solution during reheating before entering absorber. Absorbing steam, the initial solution has been reformed in the absorber. This alternative is preferred when the solute has endothermic heat of solution. In any case, heat transfer takes place between solutions that are cooled and solutions that are heated. During dissolution of separated phase in the collector, heat is rejected at high temperature in case solute with exothermic heat of solution is selected. This heat may be used for solution heating too. Part of the steam may be absorbed by the separated phase at low temperature. In this alternative additional heat is needed for vaporization. The steam produced from evaporator is superheated and expands through a turbine (TU1) producing mechanical work. The expansion pressure corresponds to the desired heating temperature. Next the steam is condensed through heat exchanger (CO), expanded at the desired refrigerator pressure and evaporates through heat exchanger (EV). The steam is superheated and compressed again through compressor (TU2) and driven to absorber to be condensed. Compressor (TU2) is helped by the work of turbine (TU1). These compressor and turbine are used to regulate heating and refrigeration temperature. Water and organic solvents like DMSO, Methanol, monomethylamine, dimethilsulfoxide, DMF, acetonitrile, formamide, formic acid may be used as solvent and electrolytes like CoI2, Pb(NO3)2, TICl, RbNO3, TINO3, ZnCl2, SbCl2, SbF2, (Cl, Br, I, SO4) with (K, Na, NH4, Li) may be used as solutes.
 5. A method of heat compression of a working fluid for heat transfer to higher temperature as in claim 4, characterized by the combination of many such cycles. The steam produced by the evaporator of the first cycle is absorbed by the absorber of the second. The steam from the evaporator of the second cycle is absorbed by the absorber of the first. Temperature levels are selected so as heat rejected during condensations is utilized for evaporations. The pressure levels are selected so that evaporator of the second cycle is at the same level with absorber of the first. Steam is compressed in case absorber works at a little higher pressure. A higher temperature lift is achieved.
 6. A method of heat compression of a working fluid by solution concentration change as in claim 5 characterized by the fact that the steam produced by the first evaporator is expanded through a turbine to produce work instead of performing the cooling cycle. After expansion, the steam is absorbed by the absorber. Part of the steam may be absorbed at low temperature by the separated phase too.
 7. A method of heat compression of a working fluid for heat transfer by solution concentration change as in claim 1, characterized by the fact that a solute which concentration decreases when temperature increases is used. An example is KBr with NH3. The higher concentration solution is at low temperature. The solution is heated to a higher temperature and solute is separated and selected to container (K). The solution is vaporized at high temperature consuming heat. The steam performs the cooling cycle of condensation—expansion—evaporation and is absorbed by the absorber at the low temperature. The remaining solution from the evaporator is driving to absorber while the solute is dissolved into this to form the initial high concentration solution. Steam may be absorbed by part of the separated phase at low temperature too. Heat exchange takes place between the two solutions moving the opposite direction. Lower pressure compression is needed for the same temperature lift of the conventional cycle. A gaseous solute like Freon or NH3 may be used beyond electrolytes. The method is useful especially when solute which molecules are connected with solvent molecules only at low temperature is used. Addition heat is consumed for evaporation.
 8. A method for fluid compression as in claim 7 characterized by the fact that the steam is expanded through a turbine to produce work instead of performing the cooling cycle. 